CN113750953A - SO in pyrolysis flue gas2、H2S and Hg0Synergistic desorption adsorbent and preparation method thereof - Google Patents
SO in pyrolysis flue gas2、H2S and Hg0Synergistic desorption adsorbent and preparation method thereof Download PDFInfo
- Publication number
- CN113750953A CN113750953A CN202111136193.XA CN202111136193A CN113750953A CN 113750953 A CN113750953 A CN 113750953A CN 202111136193 A CN202111136193 A CN 202111136193A CN 113750953 A CN113750953 A CN 113750953A
- Authority
- CN
- China
- Prior art keywords
- gamma
- adsorbent
- ferric
- flue gas
- mercury
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/06—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group B01J20/04
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Landscapes
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Catalysts (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
The invention discloses SO in pyrolysis flue gas2、H2S and Hg0A synergistic desorption adsorbent and a process for its preparation, comprising gamma-Al2O3Particulate carrier and carrier supported on gamma-Al2O3A mixture of cerium oxide and iron oxide on a particulate support. The catalytic adsorbent can realize H in pyrolysis flue gas2The removal rate of S is more than 95 percent, and SO2The optimal removal rate of the mercury reaches more than 70 percent, and the optimal removal rate of the mercury reaches more than 95 percent. The ultrasonic dipping method is characterized in that the ultrasonic effect is utilized to strengthen the uniform distribution of the active components, and the loading capacity of the active components is increased.
Description
Technical Field
The invention belongs to the technical field of pyrolysis flue gas purification, and particularly relates to SO in pyrolysis flue gas2、H2S and Hg0A synergistic desorption adsorbent and a preparation method thereof.
Background
The statements herein merely provide background information related to the present disclosure and may not necessarily constitute prior art.
The environmental pollution caused by the emission of the coal-fired pollutants increasingly affects the life of human beings, and the efficient clean utilization of the coal is more and more concerned and valued by the nation. At present, SO in coal-fired flue gas2、NOxAnd dust are effectively controlled, but the existing technology for controlling the emission of mercury in flue gas cannot realize industrial application. The mercury is a poisonous and harmful heavy metal which is extremely easy to volatilize, the elementary substance mercury is stable in form and can exist in the atmosphere for a long time, and the mercury can be transported for a long distance to form large-scale mercury pollution. The emission standard of atmospheric pollutants for boilers issued in 2014 stipulates that the maximum allowable emission concentration limit of mercury and compounds thereof in boiler flue gas is 0.05mg/m3. The development of economic and efficient coal-fired mercury control technology with development prospect, particularly mercury simple substance, is one of the important problems to be solved urgently in the current clean coal-fired technology.
By means of heat treatment technology, raw coal is pyrolyzed at low temperature before being burnt, volatile pollutant substances in the coal can be removed, and the pollutant substances comprise high-concentration sulfur compounds, mercury compounds and the like. The research foundation of the American Iowa State university researches that the raw coal powder is subjected to mild pyrolysis by using the recovered hot flue gas, most of mercury in the raw coal is released, and mercury vapor in the recovered flue gas is removed from the pyrolysis flue gas through the conventional flue gas treatment device, so that the aim of removing mercury before combustion is fulfilled (Zhang Cheng, Caona, and the like, research on release characteristics of mild pyrolysis mercury and sulfur before coal combustion, China Motor engineering Proc, 2009, 29 (20): 35-40.). Compared with the flue gas demercuration technology, the efficiency of heat treatment demercuration before combustion is greatly improved, and other harmful elements such as arsenic, selenium and the like in coal can be released into pyrolysis flue gas. However, the inventor finds that the produced pyrolysis flue gas in the technology is removed mercury and other pollutants in advance by a certain technical means before entering the furnace for combustion, and can greatly reduce the burden and the operation cost of the coal-fired flue gas pollutant treatment device. In addition, although related adsorbents are developed to remove mercury, hydrogen sulfide and other substances in hot gas in the prior art, the inventor finds that related technology processes only aim at one pollutant, neglect the inherent correlation of sulfur and mercury elements in pyrolysis flue gas, and the conventional adsorbents are difficult to achieve the synergistic removal of sulfur dioxide, hydrogen sulfide and mercury elements. Meanwhile, the method also has the problems of high price of the adsorbent, high demercuration cost, easy reduction of the adsorption capacity of the adsorbent, high ignition loss rate, easy reduction of mechanical strength and the like.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide SO in pyrolysis flue gas2、H2S and Hg0A synergistic desorption adsorbent and a preparation method thereof.
In order to achieve the purpose, the invention is realized by the following technical scheme:
in a first aspect, the invention provides SO in pyrolysis flue gas2、H2S and Hg0Synergistic desorption of adsorbents including gamma-Al2O3Particulate carrier and carrier supported on gamma-Al2O3Or TiO2A mixture of cerium oxide and iron oxide on a particulate support.
In some embodiments, the adsorbent comprises 1-8% by weight cerium oxide and 1-15% by weight iron oxide.
In some embodiments, γ -Al2O3The particle size of the particulate carrier is 100-1000 μm, preferably 100-800 μm.
The inventor finds that the grain diameter is 100-2O3Or TiO2The particulate carrier has the function of a catalyst and strengthens low-concentration SO2And H2The reaction under S is as follows: SO (SO)2+2H2S→3S+2H2O，2H2S+O2→2S+2H2The O, the ferric oxide and the cerium oxide have the function of an auxiliary agent, and can promote the transfer of surface active oxygen of two chemical reactions, further promote the forward proceeding of the two reactions, and effectively reduce the SO in the pyrolysis flue gas2The concentration of (c).
Elemental mercury in pyrolysis flue gas is in a micro-oxygen environment (under a micro-oxygen atmosphere, an adsorbent surface)The stored oxygen of the noodle is rich, the adsorbed elemental mercury and active oxygen are easy to generate oxidation reaction), part of the adsorbed elemental mercury is adsorbed, part of the adsorbed elemental mercury is oxidized, and the Hg in the adsorbed elemental mercury is enriched0Or Hg2+With S or H2S is subjected to adsorption reaction to generate HgS, so that the mercury in the flue gas is greatly reduced in emission control difficulty while the synergistic removal of sulfur and mercury is realized.
SO in pyrolysis flue gas2、H2S and Hg0The efficiency of coal-fired demercuration and desulfurization is effectively improved by synergistic removal, and the treatment cost of mercury is greatly reduced by matching with the existing coal-fired flue gas pollutant equipment.
In a second aspect, the invention provides SO in the pyrolysis flue gas2、H2S and Hg0The preparation method of the synergistic desorption adsorbent comprises the following steps:
mixing gamma-Al2O3Dipping the particles in a mixed solution of ferric salt and trivalent cerium salt, and performing ultrasonic dipping; and drying and roasting the impregnated solid to obtain the adsorbent.
In some embodiments, the ferric salt is ferric nitrate or ferric chloride and the ferric cerium salt is cerium nitrate or cerium chloride.
Further, the weight percentage of the ferric salt is 1-15%, preferably 3-10%;
the mass percent of the trivalent cerium salt is 1-8%, preferably 2-6%.
In some embodiments, the power of ultrasonic immersion is 10-100W and the time of ultrasonic immersion is 1-6 h.
In some embodiments, the drying is first drying at 75-85 ℃ for 1-3h, and then drying at 95-105 ℃ for 1-3 h. The rapid evaporation of water can carry the impregnated nitrate to the surface of the porous material, so that the internal distribution is uneven, sintering is easily generated after roasting, the quality of the adsorbent is influenced, and the problems can be effectively solved by step drying.
In some embodiments, the temperature of the calcination is 400-600 ℃, and the calcination time is 3-5 h.
The beneficial effects of the invention are as follows:
the catalytic adsorbent can realize H in pyrolysis flue gas2The removal rate of S is 95 percentAbove, SO2The optimal removal rate of the mercury reaches more than 70 percent, and the optimal removal rate of the mercury reaches more than 95 percent.
The ultrasonic dipping method is characterized in that: the ultrasonic effect is utilized to strengthen the uniform distribution of the active components, and simultaneously, the loading capacity of the active components is increased.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 shows that the catalytic adsorbent U60Fe10Ce 6/gamma-Al prepared in example 22O3Evaluating the mercury removal efficiency;
FIG. 2 shows that the catalytic adsorbent U60Fe10Ce 6/gamma-Al prepared in example 22O3Evaluating the hydrogen sulfide removal efficiency;
FIG. 3 shows that the catalytic adsorbent U60Fe10Ce 6/gamma-Al prepared in example 22O3Evaluation results of sulfur dioxide removal efficiency.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
The present invention will be further described with reference to the following specific examples.
Example 1
Gamma-Al carrier with grain diameter of 300-450 mu m2O3Drying at 100 deg.C for 3 hr in vacuum drying oven, and weighing 10g pretreated carrier gamma-Al2O3Mixing with 50ml of ferric chloride solution with the mass concentration of 6% and cerium chloride solution with the mass concentration of 3% into a conical flask, placing the impregnation solution containing the carrier into an ultrasonic cleaning instrument, ultrasonically impregnating for 3 hours with the ultrasonic power of 30W, filtering a sample, drying at 80 ℃ and 100 ℃ for 2 hours respectively, roasting in a muffle furnace at 500 ℃ for 3 hours, and naturally cooling to room temperature to obtain a catalytic adsorbent U30Fe6Ce 3/gamma-Al2O3。
The prepared catalytic adsorbent U30Fe6Ce 3/gamma-Al2O3Placing in a fixed bed reactor, wherein the reaction gas comprises the following components: 600ppm H2S，300ppm SO2，50μg/m3 Hg0，20vol％H2，15vol％CO，5vol％CO2，3vol％H2O, balance gas N2The reaction temperature is 120 ℃, and the reaction space velocity is 5000h-1. Hg at 180min of reaction0The removal rate is more than 75 percent, the mercury capacity is 1.8mg/g, H2The S removal efficiency is more than 95 percent, and SO2The removal efficiency is more than 50%.
Example 2
Gamma-Al carrier with grain diameter of 300-450 mu m2O3Drying at 100 deg.C for 3 hr in vacuum drying oven, and weighing 10g pretreated carrier gamma-Al2O3Mixing with 50ml of 10% ferric chloride and 6% cerium chloride solution, placing the impregnation solution containing the carrier in an ultrasonic cleaning instrument, ultrasonically impregnating for 3h with the ultrasonic power of 60W, filtering the sample, drying at 80 ℃ and 100 ℃ for 2h respectively, roasting in a muffle furnace at 500 ℃ for 3h, and naturally cooling to room temperature to obtain a catalytic adsorbent U60Fe10Ce 6/gamma-Al2O3。
The prepared catalytic adsorbent U60Fe10Ce 6/gamma-Al2O3Placing in a fixed bed reactor, wherein the reaction gas comprises the following components: 600ppm H2S，300ppm SO2，50μg/m3 Hg0，20vol％H2，15vol％CO，5vol％CO2，3vol％H2O, balance gas N2The reaction temperature is 120 ℃, and the reaction space velocity is 5000h-1. Hg at 180min of reaction0The removal rate is more than 80 percent, the mercury capacity is 2.3mg/g, H2The S removal efficiency is more than 95 percent, and SO2The removal efficiency is more than 60%.
Example 3
Gamma-Al carrier with grain diameter of 300-450 mu m2O3Drying at 100 deg.C for 3 hr in vacuum drying oven, and weighing 10g pretreated carrier gamma-Al2O3With 10 percent of ferric nitrate and 6 percent of cerous nitrate solution 50 by mass concentrationml is mixed into a conical flask, the impregnation solution containing the carrier is placed into an ultrasonic cleaning instrument for ultrasonic impregnation for 3h, the ultrasonic power is 60W, then a sample is filtered, the sample is dried for 2h at 80 ℃ and 100 ℃ respectively, then the sample is roasted for 3h at 500 ℃ in a muffle furnace, and the catalytic adsorbent U60Fe10Ce 6/gamma-Al is obtained after natural cooling to the room temperature2O3(N)。
The prepared catalytic adsorbent U60Fe10Ce 6/gamma-Al2O3(N) placing in a fixed bed reactor, wherein the reaction gas composition is as follows: 600ppm H2S，300ppm SO2，50μg/m3 Hg0，20vol％H2，15vol％CO，5vol％CO2，3vol％H2O, balance gas N2The reaction temperature is 120 ℃, and the reaction space velocity is 5000h-1. Hg at 180min of reaction0The removal rate is more than 70 percent, the mercury capacity is 1.6mg/g, H2The S removal efficiency is more than 95 percent, and SO2The removal efficiency is more than 50%.
Example 4
Gamma-Al carrier with grain diameter of 300-450 mu m2O3Drying at 100 deg.C for 3 hr in vacuum drying oven, and weighing 10g pretreated carrier gamma-Al2O3Mixing with 50ml of 10% ferric chloride and 6% cerium chloride solution, placing the impregnation solution containing the carrier in an ultrasonic cleaning instrument, ultrasonically impregnating for 3h with the ultrasonic power of 60W, filtering the sample, drying at 80 ℃ and 100 ℃ for 2h respectively, roasting in a muffle furnace at 500 ℃ for 3h, and naturally cooling to room temperature to obtain a catalytic adsorbent U60Fe10Ce 6/gamma-Al2O3。
The prepared catalytic adsorbent U60Fe10Ce 6/gamma-Al2O3Placing in a fixed bed reactor, wherein the reaction gas comprises the following components: 600ppm H2S，300ppm SO2，50μg/m3 Hg0，20vol％H2，15vol％CO，5vol％CO2，3vol％H2O, balance gas N2The reaction temperature is respectively 200 ℃ and 300 ℃, and the reaction space velocity is 2000h-1. When the reaction is carried out for 180min, the mercury removal rate is respectively over 52 percent and 41 percent, the mercury capacity is respectively 1.1 mg/g and 0.85mg/g, and H2S removal efficiency is equalOver 90% of SO2The removal efficiency is more than 40% and 30%.
Example 5
Gamma-Al carrier with grain diameter of 300-450 mu m2O3Drying at 100 deg.C for 3 hr in vacuum drying oven, and weighing 10g pretreated carrier gamma-Al2O3Mixing with 50ml of 10% ferric chloride and 6% cerium chloride solution, placing the impregnation solution containing the carrier in an ultrasonic cleaning instrument, ultrasonically impregnating for 3h with the ultrasonic power of 60W, filtering the sample, drying at 80 ℃ and 100 ℃ for 2h respectively, roasting in a muffle furnace at 500 ℃ for 3h, and naturally cooling to room temperature to obtain a catalytic adsorbent U60Fe10Ce 6/gamma-Al2O3。
The prepared catalytic adsorbent U60Fe10Ce 6/gamma-Al2O3Placing in a fixed bed reactor, wherein the reaction gas comprises the following components: 600ppm H2S，300ppm SO2，50μg/m3 Hg0，20vol％H2，15vol％CO，5vol％CO2，3vol％H2O，3vol％O2The reaction temperature of the equilibrium gas N2 is 120 ℃ respectively, and the reaction space velocity is 5000h-1. The mercury removal rate is more than 70 percent when the reaction is carried out for 180min, H2The S removal efficiency is over 95 percent, and SO2The removal efficiency is more than 40%.
Comparative example 1
The difference from example 2 is that: support gamma-Al2O3The particle diameter of (A) was 1mm to 3mm, and the rest was the same as in example 1.
Hg0The removal rate is 72 percent, the mercury capacity is 1.95mg/g, H2S removal efficiency of 83%, SO2The removal efficiency was 47%.
Comparative example 2
The difference from the example 2 lies in: the procedure of example 1 was repeated except that "50 ml of a 10% ferric chloride and 6% cerium chloride solution" was replaced with "50 ml of a 16% ferric chloride solution".
Hg0The removal rate is 76 percent, the mercury capacity is 2.03mg/g, H2The S removal efficiency was 87%, SO2The removal efficiency was 43%.
Comparative example 3
The difference from the example 2 lies in: the procedure of example 1 was repeated except that "50 ml of a 10% ferric chloride and 6% cerium chloride solution" was replaced with "50 ml of a 16% cerium chloride solution".
Hg0The removal rate is 75 percent, the mercury capacity is 1.8mg/g, H2S removal efficiency of 61%, SO2The removal efficiency was 35%.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. SO in pyrolysis flue gas2、H2S and Hg0The synergistic desorption adsorbent is characterized in that: comprising gamma-Al2O3Particulate carrier and carrier supported on gamma-Al2O3A mixture of cerium oxide and iron oxide on a particulate support.
2. SO in pyrolysis flue gas according to claim 12、H2S and Hg0The synergistic desorption adsorbent is characterized in that: in the adsorbent, the mass percent of cerium oxide is 1-8%, and the mass percent of ferric oxide is 1-15%.
3. SO in pyrolysis flue gas according to claim 12、H2S and Hg0The synergistic desorption adsorbent is characterized in that: gamma-Al2O3The particle size of the particulate carrier is 100-1000 μm, preferably 100-800 μm.
4. SO in pyrolysis flue gas of claim 12、H2S and Hg0The preparation method of the synergistic desorption adsorbent is characterized by comprising the following steps: the method comprises the following steps:
mixing gamma-Al2O3Fine particle impregnationSoaking in mixed solution of ferric iron salt and ferric cerium salt, and ultrasonic soaking; and drying and roasting the impregnated solid to obtain the adsorbent.
5. The method of claim 4, wherein: the ferric salt is ferric nitrate or ferric chloride, and the ferric cerium salt is cerous nitrate or cerous chloride.
6. The method of claim 4, wherein: the weight percentage of the trivalent ferric salt is 1-15%, preferably 3-10%.
7. The method of claim 4, wherein: the mass percent of the trivalent cerium salt is 1-8%, preferably 2-6%.
8. The method of claim 4, wherein: the power of ultrasonic dipping is 10-100W, and the time of ultrasonic dipping is 1-6 h.
9. The method of claim 4, wherein: the drying is to dry for 1-3h at 75-85 ℃ and then dry for 1-3h at 95-105 ℃.
10. The method of claim 4, wherein: the roasting temperature is 400-600 ℃, and the roasting time is 3-5 h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111136193.XA CN113750953B (en) | 2021-09-27 | 2021-09-27 | SO in pyrolysis flue gas 2 、H 2 S and Hg 0 Synergistic desorption adsorbent and preparation method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111136193.XA CN113750953B (en) | 2021-09-27 | 2021-09-27 | SO in pyrolysis flue gas 2 、H 2 S and Hg 0 Synergistic desorption adsorbent and preparation method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113750953A true CN113750953A (en) | 2021-12-07 |
| CN113750953B CN113750953B (en) | 2023-07-21 |
Family
ID=78797805
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111136193.XA Active CN113750953B (en) | 2021-09-27 | 2021-09-27 | SO in pyrolysis flue gas 2 、H 2 S and Hg 0 Synergistic desorption adsorbent and preparation method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113750953B (en) |
Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3855387A (en) * | 1973-09-05 | 1974-12-17 | St Joe Minerals Corp | Method for removing mercury from industrial gases |
| JP2003138277A (en) * | 2001-10-31 | 2003-05-14 | Mitsubishi Heavy Ind Ltd | Mercury removal method and its system |
| CN1431048A (en) * | 2001-11-23 | 2003-07-23 | 中国科学院山西煤炭化学研究所 | Load typed iron catalyst and its preparing method and application |
| US7060233B1 (en) * | 2002-03-25 | 2006-06-13 | Tda Research, Inc. | Process for the simultaneous removal of sulfur and mercury |
| US20080307779A1 (en) * | 2005-07-12 | 2008-12-18 | El-Mekki El-Malki | Regenerable sulfur traps for on-board vehicle applications |
| CN102430383A (en) * | 2011-11-04 | 2012-05-02 | 太原理工大学 | Preparation method of adsorbing agent simultaneously removing H2S and Hg in middle temperature coal gas |
| CN102764629A (en) * | 2012-08-17 | 2012-11-07 | 太原理工大学 | Method for preparing absorbing agent for medium-temperature gas desulfurization |
| US20130204064A1 (en) * | 2012-02-06 | 2013-08-08 | Uop Llc | Method of Making Supported Copper Adsorbents Having Copper at Selectively Determined Oxidation Levels |
| CN103691313A (en) * | 2013-12-19 | 2014-04-02 | 华中科技大学 | Method and device for removing mercury through catalytic oxidation |
| CN104226248A (en) * | 2014-09-04 | 2014-12-24 | 太原理工大学 | Preparation method of semicoke-loaded manganin adsorbing agent and application of adsorbing agent |
| CN106492821A (en) * | 2016-09-28 | 2017-03-15 | 北京科技大学 | A kind of efficient cryogenic sulfur resistive water resistant cooperates with the preparation method of denitration demercuration catalyst |
| CN106732541A (en) * | 2016-12-07 | 2017-05-31 | 盐城复华环保产业开发有限公司 | The method that ultrasonic wave infusion process prepares low-temperature selective catalytic reduction denitration catalyst |
| WO2017181815A1 (en) * | 2016-04-21 | 2017-10-26 | 武汉凯迪工程技术研究总院有限公司 | Supported iron-based catalyst for fischer-tropsch synthesis and manufacturing method thereof |
| US20190060862A1 (en) * | 2017-08-28 | 2019-02-28 | Viviron Technology LLC | Iron-Selenide-Oxide Sorbent Composition for Removing Mercury (Hg) Vapor from a Gaseous stream; Methods of Use and Methods of Manufacture |
| CN109758904A (en) * | 2019-01-10 | 2019-05-17 | 昆明理工大学 | A kind of method of ultraviolet cooperating low-temperature catalytic oxidation processing non-ferrous metal metallurgy flue gas acid preparing tail gas |
| CN110270342A (en) * | 2019-07-04 | 2019-09-24 | 南京大学 | A kind of iron cerium aluminum oxide catalyst, preparation method and applications |
| CN113019094A (en) * | 2021-03-09 | 2021-06-25 | 徐州工程学院 | Device and method for efficiently removing mercury by using sulfur-containing waste gas |
-
2021
- 2021-09-27 CN CN202111136193.XA patent/CN113750953B/en active Active
Patent Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3855387A (en) * | 1973-09-05 | 1974-12-17 | St Joe Minerals Corp | Method for removing mercury from industrial gases |
| JP2003138277A (en) * | 2001-10-31 | 2003-05-14 | Mitsubishi Heavy Ind Ltd | Mercury removal method and its system |
| CN1431048A (en) * | 2001-11-23 | 2003-07-23 | 中国科学院山西煤炭化学研究所 | Load typed iron catalyst and its preparing method and application |
| US7060233B1 (en) * | 2002-03-25 | 2006-06-13 | Tda Research, Inc. | Process for the simultaneous removal of sulfur and mercury |
| US20080307779A1 (en) * | 2005-07-12 | 2008-12-18 | El-Mekki El-Malki | Regenerable sulfur traps for on-board vehicle applications |
| CN102430383A (en) * | 2011-11-04 | 2012-05-02 | 太原理工大学 | Preparation method of adsorbing agent simultaneously removing H2S and Hg in middle temperature coal gas |
| US20130204064A1 (en) * | 2012-02-06 | 2013-08-08 | Uop Llc | Method of Making Supported Copper Adsorbents Having Copper at Selectively Determined Oxidation Levels |
| CN102764629A (en) * | 2012-08-17 | 2012-11-07 | 太原理工大学 | Method for preparing absorbing agent for medium-temperature gas desulfurization |
| CN103691313A (en) * | 2013-12-19 | 2014-04-02 | 华中科技大学 | Method and device for removing mercury through catalytic oxidation |
| CN104226248A (en) * | 2014-09-04 | 2014-12-24 | 太原理工大学 | Preparation method of semicoke-loaded manganin adsorbing agent and application of adsorbing agent |
| WO2017181815A1 (en) * | 2016-04-21 | 2017-10-26 | 武汉凯迪工程技术研究总院有限公司 | Supported iron-based catalyst for fischer-tropsch synthesis and manufacturing method thereof |
| CN106492821A (en) * | 2016-09-28 | 2017-03-15 | 北京科技大学 | A kind of efficient cryogenic sulfur resistive water resistant cooperates with the preparation method of denitration demercuration catalyst |
| CN106732541A (en) * | 2016-12-07 | 2017-05-31 | 盐城复华环保产业开发有限公司 | The method that ultrasonic wave infusion process prepares low-temperature selective catalytic reduction denitration catalyst |
| US20190060862A1 (en) * | 2017-08-28 | 2019-02-28 | Viviron Technology LLC | Iron-Selenide-Oxide Sorbent Composition for Removing Mercury (Hg) Vapor from a Gaseous stream; Methods of Use and Methods of Manufacture |
| CN109758904A (en) * | 2019-01-10 | 2019-05-17 | 昆明理工大学 | A kind of method of ultraviolet cooperating low-temperature catalytic oxidation processing non-ferrous metal metallurgy flue gas acid preparing tail gas |
| CN110270342A (en) * | 2019-07-04 | 2019-09-24 | 南京大学 | A kind of iron cerium aluminum oxide catalyst, preparation method and applications |
| CN113019094A (en) * | 2021-03-09 | 2021-06-25 | 徐州工程学院 | Device and method for efficiently removing mercury by using sulfur-containing waste gas |
Non-Patent Citations (7)
| Title |
|---|
| PENGYING WANG ET AL: "Catalytic oxidation of Hg0 by MnOx–CeO2/γ-Al2O3 catalyst at low temperatures", CHEMOSPHERE, vol. 101 * |
| TINGTING GE ET AL: ""Sulfur production from smelter off-gas using CO-H2 gas mixture as the reducing agent over modified Fe/γ-Al2O3 catalysts"", 《CHINESE JOURNAL OF CHEMICAL ENGINEERING》, vol. 26, pages 2 * |
| YAN LIU ET AL: ""Effect of CeO2 doping on catalytic activity of Fe2O3/γ-Al2O3 catalyst for catalytic wet peroxide oxidation of azo dyes"", 《JOURNAL OF HAZARDOUS MATERIALS》, vol. 143, pages 2 * |
| 孙敬方等: ""现代表征技术在研究多相催化剂Fe2O3-CeO2/γ-Al2O3的结构和CO氧化反应性能中的应用"", 《应用化工》, vol. 49, pages 1867 * |
| 张亚平等: ""光Fenton反应的Ce-Fe/Al2O3催化剂超声制备及性能表征"", 《中国有色金属学报》, vol. 17, pages 1 * |
| 张惠灵等: ""微波诱导催化剂Fe2O3-CeO2/γ-Al2O3的制备及其对甲基橙的催化降解性能"", 《化工环保》, vol. 28, pages 1 * |
| 谢亚婷: "Mn、Ce改性γ-Al2O3催化剂脱除燃煤烟气汞及其抗硫特性实验研究", 中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑, no. 06 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113750953B (en) | 2023-07-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Tian et al. | Removal of elemental mercury by activated carbon impregnated with CeO2 | |
| Shen et al. | Metal chlorides loaded on activated carbon to capture elemental mercury | |
| JP3272367B2 (en) | Heat-treated activated carbon fiber for denitration, method for producing the same, denitration method using the same, and denitration system using the same | |
| CN109529885B (en) | Cobalt sulfide/biomass charcoal composite material, preparation method thereof and application of cobalt sulfide/biomass charcoal composite material as elemental mercury oxidation catalyst | |
| CN110252255B (en) | Preparation method and application of gaseous mercury adsorbent | |
| CN104307539B (en) | A catalyst used for oxidation of elementary substance mercury in coal-fired flue gas, and a preparation method and a regeneration method of the catalyst | |
| Zhang et al. | Simultaneous NO/CO2 removal by Cu-modified biochar/CaO in carbonation step of calcium looping process | |
| CN108499340A (en) | A kind of Mercury In Coal Combustion Flue Gas removing recycling and adsorbent regeneration method based on CLP processes | |
| CN114057193A (en) | Nitrogen-doped activated carbon-based desulfurizer as well as preparation method and application thereof | |
| CN114259978A (en) | Preparation process of efficient coal-fired flue gas demercuration adsorbent and product thereof | |
| JP2007529305A (en) | Method for reducing heavy metals in flue gas | |
| CN107159088B (en) | Mercury-containing material with lasting adsorption performance | |
| CN108654633B (en) | Low-temperature denitration catalyst and preparation method and use method thereof | |
| CN113797894B (en) | Supported porous carbon material, preparation method thereof and application thereof in flue gas dearsenification | |
| CN109200812B (en) | Method for removing gaseous mercury in flue gas by catalytic oxidation of cobalt sulfide/biomass charcoal composite material | |
| CN108993504B (en) | Modified activated coke for demercuration of sulfur-containing flue gas and preparation method thereof | |
| CN110115975A (en) | Modified carbon nitride adsorbent of a kind of manganese oxide and the preparation method and application thereof | |
| CN112691542B (en) | Metal composite molecular sieve material for adsorbing-catalytically oxidizing VOCs (volatile organic compounds), and preparation method and application thereof | |
| CN106237982A (en) | CuO/ attapulgite catalyst-sorbent and for removing the method for Elemental Mercury in flue gas | |
| CN102764655A (en) | Novel demercuration catalyst | |
| Zhang et al. | NO removal performance of CO in carbonation stage of calcium looping for CO2 capture | |
| CN113750953B (en) | SO in pyrolysis flue gas 2 、H 2 S and Hg 0 Synergistic desorption adsorbent and preparation method thereof | |
| CN109158082B (en) | Demercuration method based on porous carbon online activation | |
| JP2004066009A (en) | Carbon material and equipment for treating flue gas | |
| JP2002529225A (en) | Catalyst body and method for reducing halogenated hydrocarbons |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |